Process for separating internal and alpha olefins from saturated compounds

ABSTRACT

A process for separating and isolating saturated hydrocarbons from olefins, and in particular, a process for separating and isolating saturated hydrocarbons from olefins in a Fisher-Tropsch stream. The feedstock composition is contacted with linear polyaromatic compound under conditions effective to form linear polyaromatic compound-olefin adducts. Separation of the adducts from the stream also separates the adducted olefins from the stream. After dissociation of the adducted olefins, the process results in an olefin composition that is enriched in concentration of olefins over the concentration of olefins in the feedstock composition, and a saturated hydrocarbon stream that is enriched in saturated hydrocarbons over the concentration of saturated hydrocarbons in the feedstock.

This is a division of application Ser. 09/379,089 filed Aug. 23, 1999,now U.S. Pat. No. 6,184,431 the entire disclosure of which is herebyincorporated by reference.

1. FIELD OF THE INVENTION

This invention relates to a process for separating olefins fromsaturated hydrocarbons followed by separating linear alpha olefins andinternal olefins from a saturated hydrocarbon stream.

2. BACKGROUD OF THE INVENTION

Many industrial processes produce olefin/saturated hydrocarbon streamsthat are mixtures of olefins, saturated hydrocarbons, and oxygenates.Olefins are frequently used in the manufacture of polymers such aspolyethylene, as drilling mud additives, or as intermediates for theproduction of oil additives and detergents. Some industrial processesmanufacture olefin streams by oligomerizing ethylene over an alphaolefin catalyst to produce mixtures of alpha and internal olefins havinga broad range of carbon numbers. However, these streams rely on the useof ethylene as a feedstock material, which add a significant cost to themanufacture of the olefin. On the other hand, the FT process starts withan inexpensive feedstock, syngas, generally derived from natural gas,coal, coke, and other carbonaceous compounds to make oligomers comprisedof olefins, aromatics, saturates, and oxygenates.

The FT process, however, is not very selective to the production ofolefins. While reaction conditions and catalysts can be tuned tomanufacture a stream rich in the desired species within the FT productstream, a large percentage of the FT stream contains other types ofcompounds which must be separated from the olefins, which olefins arepurified, and then sold into different markets. For example, a typicalcommercial FT stream will contain a mixture of saturated hydrocarbons,olefins, aromatics, and oxygenates such as organic carboxylic acids,alcohols, ethers, esters, ketones, and aldehydes. All these compoundsmust be separated from the crude FT stream before a particularcomposition may be offered commercially. To further complicate theseparation operation, the FT stream contains compounds having a widespectrum of carbon numbers, as well as a wide variety of olefins,ranging from C₂-C₂₀₀ species, internal linear olefins, alpha linearolefins, internal branched olefins, alpha branched olefins, and cyclicolefins, many of which have similar molecular weights. Separating andisolating these species is no easy task. Conventional distillationmethods are frequently inadequate to separate species having closelyrelated boiling points.

Various processes have been proposed to efficiently separate thedifferent species in an FT stream with sufficient purity that aparticular composition is acceptable in the intended application. Theseprocesses for separating out different species in an FT stream includethe use of molecular sieves, which are restricted to a feed have anaverage carbon number range which is more limited than a compositioncontaining a broad spectrum of average carbon numbers ranging fromC₅-C₂₀, to the use of exchange resins, to the use of super-fractionatorsoften operated at high pressure, and the use of oligomerizationcatalysts or etherification techniques to alter the boiling points ofthe species in the FT stream. Many reactive methods for separatingspecies in an FT stream do not, however, selectively react with olefinswhile simultaneously reject paraffins.

U.S. Pat. No. 4,946,560 described a process for the separation ofinternal olefins from alpha olefins by contacting a feedstock with anadducting compound such as anthracene to form an olefin adduct,separating the adduct from the feedstock, dissociating the olefin adductthrough heat to produce anthracene and an olefin composition enriched inalpha olefin, and separating out the anthracene from the alpha olefin.This reference does not suggest the desirability or the capability ofanthracene to separate olefins from saturated hydrocarbons or linearalpha olefins from saturated hydrocarbons.

Once olefins are separated from saturated hydrocarbons, it would also bedesirable to purify the removed saturated hydrocarbons and extract asmuch remaining olefin from the removed saturated hydrocarbon aspossible.

3. SUMMARY OF THE INVENTION

This invention relates to a process for separating olefins fromsaturated hydrocarbons, and thereafter further treating the olefins toseparate olefins from a stream of saturated hydrocarbons. The process ofthe invention is well suited to treating a FT stream.

In particular, there is provided a process for treating a feedstockcomposition comprising linear alpha olefins, internal olefins, andsaturated hydrocarbons, comprising:

a) contacting the feedstock composition with a linear polyaromaticcompound in a first reaction zone under conditions effective to form areaction mixture comprising linear polyaromatic compound-olefin adductsand saturated hydrocarbons;

b) separating the first linear polyaromatic compound-olefin adducts fromthe saturated hydrocarbons in the reaction mixture to form an adductedolefin stream and a first saturated hydrocarbon stream enriched in theconcentration of saturated hydrocarbons over the concentration ofsaturated hydrocarbons in the feedstock composition;

si) contacting the saturated hydrocarbon stream with a linearpolyaromatic compound in a second reaction zone under conditionseffective to form a reaction mixture comprising second linearpolyaromatic compound-olefin adducts and saturated hydrocarbons;

sii) separating the second linear polyaromatic compound-olefin adductsfrom the saturated hydrocarbons in the reaction mixture to form a secondadducted olefin stream comprising the second linear polyaromaticcompound-olefin adducts, and a second saturated hydrocarbon streamenriched in the concentration of saturated hydrocarbons over theconcentration of saturated hydrocarbons in the first saturatedhydrocarbon stream;

siii) dissociating the second linear polyaromatic compound-olefinadducts to form linear polyaromatic compounds and a second olefincomposition comprising alpha olefins and internal olefins enriched inthe concentration of alpha olefins and internal olefins over each oftheir concentrations in the first saturated hydrocarbon stream.

4. BRIEF DESCRIPTION OF THE DRAWINGS

The FIGURE is a block flow diagram representing the process of adductingand separating a crude feedstream of olefin and saturated hydrocarbonand subjecting the separated saturated hydrocarbon stream to a furtheradducting/separation/dissociation treatment to further separate internaland linear alpha olefins from the saturated hydrocarbon stream.

5. DETAILED DESCRIPTION OF THE INVENTION

As used throughout this specification and in the claims, the term“comprising” means “at least,” such that other unmentioned elements,ingredients, or species are not excluded from the scope of invention.

The feed stream to be treated comprises at least olefins and saturatedhydrocarbons. The class of saturated hydrocarbons as used hereinincludes at least a paraffin. The class of saturated hydrocarbons mayalso include other molecules such as cycloparaffins.

An olefin means any compound containing at least one carbon-carbondouble bond. The olefins may be linear, branched, conjugated, containmultiple double bonds anywhere along the chain, substituted,unsubstituted, contain aryl or alicyclic groups, or contain heteroatoms.

The olefins may contain aryl moieties along with an aliphatic orcycloaliphatic moiety within the same compound, or may consist solely ofan aliphatic, cycloaliphatic, or cycloaliphatic with aliphatic moietieson the compound. Preferably, the olefin is an aliphatic compound.

The olefin may be branched or linear. Examples of branching includealkyl, aryl, or alicyclic branches. The number of unsaturation pointsalong the chain is also not limited. The olefin may be a mono-, di-,tri-, etc. unsaturated olefin, optionally conjugated. The olefin mayalso contain acetylenic unsaturation.

An alpha olefin is an olefin whose double bond is located on both of αand β carbon atoms. An α Carbon atom is any terminal carbon atom,regardless of how long the chain is relative to other chain lengths in amolecule. The alpha olefin may be linear or branched. Branches orfunctional groups may be located on double bond carbon atoms, on carbonatoms adjacent to the double bond carbon atoms, or anywhere else alongthe carbon backbone. The alpha olefin may also be a polyene, wherein twoor more points of unsaturation may be located anywhere along themolecule, so long as at least on double bond is in the alpha position.

An internal olefin(s) is an olefin whose double bond is located anywherealong the carbon chain except at any terminal carbon atom. The internalolefin may be linear or branched. The location of a branch orsubstitution on the internal olefin is not limited. Branches orfunctional groups may be located on the double bond carbon atoms, oncarbon atoms adjacent to the double bond carbon atoms, or anywhere elsealong the carbon backbone.

The olefin may also be substituted with chemically reactive functionalgroups. These types of compounds are identified as oxygenates. Examplesof chemically reactive functional groups are carboxyl, aldehyde, keto,thio, ether, hydroxyl, and amine. The number of functional groups on amolecule is not limited. The functional groups may be located anywherealong the carbon backbone.

The feedstock is generally produced by commercial processes such as theoligomerization of ethylene, optionally followed by isomerization anddisproportionation. Alternatively, the feedstock may be produced by theFisher-Tropsch process, which typically contains a high proportion ofparaffins. A Fisher-Tropsch process catalytically hydrogenates CO toproduce compositions containing aliphatic molecular chains. Otherprocesses for making feedstocks which may contain mixtures of olefinsand paraffins include the dehydrogenation of paraffin, such as thosemade by the Pacol™ processes of UOP, and the cracking of waxes. The mostpreferred feedstock is that obtained from a Fisher-Tropsch (FT)synthesis.

FT catalysts and reaction conditions can be selected to provide aparticular mix of species in the reaction product stream. For example,the particular catalyst and reaction conditions may be tuned to enhancethe amount of olefins and decrease the amount of paraffins andoxygenates in the stream. Alternatively, the catalyst and reactionconditions may be tuned to enhance the amount of paraffins and decreasethe amount of olefins and oxygenates in the stream.

Generally, the reaction conditions will vary depending on the type ofequipment employed. The FT reaction temperatures vary between 100° C. to500° C., an inlet gas pressure to the reactor from atmospheric to 1500psig, and an H₂/CO ratio from 0.5:1 to 5:1, preferably from 1.8:1 to2.2:1, and gas hourly space velocity ranging from 1 to 10,000 v/v/hour.A variety of reactor vessel configurations can be used, including afluidized(entrained) bed, a fixed bed, and a slurried bed. Thetemperature in these beds can be adjusted by those of ordinary skill tooptimize the formation of FT products, including hydrocarbons, andparticularly, olefins and types of olefins. To illustrate withoutlimitation, in fluidized (entrained) bed(s), the temperature of reactionis generally high—e.g. ranging from 280° to 350° C., preferably 310° to340° C. If a fixed bed reactor(s) is used, the reaction temperature isgenerally ranges within 200° C. to 200° C., preferably between 210° and240° C., and when a slurry bed reactor(s) is used, the temperature isgenerally within the range of 190° C. to 270° C.

The catalyst used in the FT process is any known in the art, butpreferably from among Mo, W, and Group VIII compounds, including iron,cobalt, ruthenium, rhodium, platinum, palladium, iridium, osmium,combinations of the foregoing, combinations with other metals, and eachbeing in the free metal form or as alloys, or as an oxide or carbide orother compound, or as a salt. Iron based and cobalt based catalysts havefound common commercial use, and ruthenium has gained importance as ametal for the catalyst which favors the formation of high melting waxyspecies under high pressure conditions. Those of skill in the artrecognize which catalysts and combinations will favor the manufacture ofdesired species in the FT reaction composition. For example, fused ironcontaining a promoter such as potassium or oxides on a silica, alumina,or silica-alumina support are known as FT synthetic catalysts. Anotherexample is the use of Co metal. Cobalt has the advantage of producingless methane during synthesis over the older nickel based catalysts, andproduces a wide spectrum of species. With the proper selection ofsupports, promoters, and other metal combinations, the cobalt catalystcan be tuned to manufacture a composition rich in the desired species.Other catalysts, such as iron-cobalt alloy catalysts, are known fortheir selectivity toward olefins under certain process conditions.

The catalysts may be fused or precipitated, or sintered, cemented,impregnated, kneading or melting onto a suitable support.

The catalysts may also contain promoters to promote the catalyst'sactivity, stability, or selectivity. Suitable promoters include alkalior alkaline earth metals, in free or combined form as an oxide,hydroxide, salt, or combinations thereof.

An FT stream generally contains virtually no sulfur or nitrogencompounds, which may be deleterious to other catalysts which derivatizethe olefins or catalyze the reaction of olefins in other oligomerizationor polymerization processes. Regardless of the method used, however, theFT process is not very selective to a particular species, and yields awide variety of species within a composition.

Examples of some of the species found in any FT stream include paraffinshaving a broad spectrum of molecular weights, alcohols, acids, ketones,and aldehydes, and small amounts of aromatics. The linear polyaromaticcompound used in the process of the invention, however, is particularlywell adapted for the separation of olefins from saturated hydrocarbonsin an FT stream in the presence of oxygenates since oxygenates do notsignificantly impair the performance of the linear polyaromaticcompound.

While reference is made to a FT stream, it is to be understood that anystream made by any process containing olefins and saturated hydrocarbonsare suitable feedstocks for the process of the invention. Most crude FTstreams contain from 5% to 95% olefins, the remainder being saturatedhydrocarbons comprising paraffins and cycloparaffins, and optionallyother compounds such as aromatics optionally containing saturated orunsaturated alkyl branches, and oxygenates, based on the weight of allingredients in the feedstock stream to the process of the invention. Thepreferred amount of olefin present in the FT stream ranges from 15 wt. %to 70 wt. %, based on the weight of the FT stream. The amount of linearalpha olefin in the FT stream is not limited, but preferably ranges from15 wt. % to 65 wt. %, based on the weight of the FT stream. The amountof other olefins, including branched olefins and internal olefins, bothlinear and branched, is also not limited, but preferably ranges from 1wt. % to 55 wt. %, more typically from 5 wt. % to 45 wt. %, based on theweight of the FT stream. The amount of paraffin in most FT streams rangefrom 5 wt. % to 99 wt. %. In some FT streams, the FT catalyst is tunedto enhance the olefin concentration and decrease the paraffinconcentration. In these streams, the amount of paraffin generally rangesfrom 5 to 65 wt. % of the stream. In other FT streams where the FTcatalyst is tuned to enhance the amount of paraffin, the amount ofparaffin in the stream ranges from 65 wt. % to 99 wt. %. The amounts ofother compounds in a FT stream, such as oxygenates and aromatics, makeup most of the remainder of the FT stream, and are generally present inamounts ranging from 5 wt. % to 40 wt. %. Minor amounts of otherby-products and impurities, less than 5 wt. %, may be present in most FTstreams. An FT stream which consists essentially of paraffins, olefins,aromatics and oxygenates can include such minor amounts of otherby-products and impurities.

The feedstock may be a processed FT stream which has been fractionatedand/or purified by a conventional distillation, extraction, or otherseparation operation to obtain a desired carbon number cut, including acomposition containing a mixture of carbon numbers or a single carboncut composition, and to remove high and low boiling compounds, includingolefins, paraffins, aromatics, and oxygenates from the crude stream.When the separation operation is conducted by distilling the reactionmixture containing the adduct, it is preferred that the feedstock usedin the process of the invention contain an average carbon number rangingfrom C₅-C₂₀ and wherein the predominant olefin species in the feedstockis within the range of C₅-C₂₀, inclusive. The polyaromatic adductingcompound efficiently separates the saturated hydrocarbons from theolefins when the average carbon number of the feedstock and thepredominant olefinic species is within this range, inclusive. When theaverage carbon number of the feedstock exceeds C₂₀, the polyaromaticcompound-olefin adduct boils at a lower temperature than many of thespecies in the C₂₀+ feedstock composition, thereby leaving these highboiling species in the reaction mixture bottoms containing the adduct.Accordingly, the particular polyaromatic compound and the particularfeedstock composition should be so selected that the polyaromaticcompound-olefin adduct composition in the reaction mixture boils at ahigher temperature than the amount of unreacted paraffin species in thefeedstock one desires to separate. Therefore, in this preferredembodiment, the feedstock stream is one which contains an average carbonnumber ranging from C₅-C₂₀, and more preferably ranging from C₆-C₁₈, andwherein the predominant olefin species is within these ranges,inclusive. These types of FT streams are generally processed by one ofthe techniques identified above to substantially remove cuts containingingredients below or exceeding the range of C₅-C₂₀.

In addition to mixtures of olefins within this range, one may alsoemploy what are known as single carbon cuts of olefins as feedstocks,wherein the single cut is within this range. For example, the feedstockemployed may be a single C₆, C₈, C₉, C₁₀, C₁₁, C₁₂, C₁₄, or C₁₆ carboncut. These carbon cuts have utility as comonomers for polyethylene, PAO,alpha olefin sulfonates, and as drilling fluids.

In the event that one desires to employ a feedstock outside of the rangeof C₅-C₂₀, other separation techniques can be used to separate theadduct from the unreacted reaction mixture, including the selection ofhigher boiling polyaromatic compounds and/or other separation techniquessuch as liquid/liquid extraction or crystallization. These techniques,of course, can also be used with feedstocks within the range of C₅-C₂₀,inclusive.

The linear polyaromatic compound is utilized in the instant process toform the adduct with the olefins in the feed stream. As used herein,“linear polyaromatic compound” refers to a linear polyaromatic compoundhaving at least three fused aromatic rings, which may be unsubstitutedor substituted and possess similar adducting properties as theunsubstituted molecule, and mixtures thereof. The linearity shouldextend to at all three of the fused rings if a three fused ring compoundis used and to at least four consecutively fused cyclic rings if a fouror more fused ring compound is used. The linear polyaromatic compoundalso refers to mixtures of compounds containing as one of theiringredients the linear polyaromatic compound, including but not limitedto coal tars, anthracene oil, and any crude mixtures containing cutsseparated from naphthalene. The linear polyaromatic compound alsoincludes aromatic molecules linked together by a bridging group, such asa hydrocarbon chain, an ether linkage, or a ketone group containingchain so long as at least three fused rings are present in a lineararrangement; as well as those containing a heteroatom which do notinterfere in the separation of olefins from saturated hydrocarbons.

The linear polyaromatic compound has a preferential selectivity towardadducting with linear alpha olefin compounds, and secondly with otherolefins, and last with paraffins, with which the compound is virtuallyunreactive under any operating condition outside of cracking conditions.The linear polyaromatic compound of choice is one which has aselectivity for linear alpha olefin compounds over other olefins greaterthan 1:1 by mole, preferably 2:1 or more, more preferably 4:1.

Non-limiting examples of the linear polyaromatic compound includeanthracene, 2,3-benzanthracene, pentacene, and hexacene. Suitableexamples of substituents on substituted linear polyaromatic compoundsinclude, but are not limited to, lower alkyl, e.g., methyl, ethyl,butyl; halo, e.g., chloro, bromo, fluoro; nitro; sulfato; sulfonyloxy;carboxyl; carbo-lower-alkoxy, e.g., carbomethoxy, carbethoxy; amino;mono- and di-lower-alkylamino, e.g., methylamino, dimethylamino,methylethylamino; amido; hydroxy; cyano; lower-alkoxy, e.g., methoxy,ethoxy; lower-alkyanoyloxy, e.g., acteoxy; monocyclic aryls, e.g.,phenyl, xylyl, toluyl, benzyl, etc. The particular substituent size,their number, and their location, should be selected so that they arerelatively inert under the reaction conditions and not so large as toblock the formation of the Diels-Alder adduct. Suitable substitutedlinear polyaromatic compounds can be determined by routineexperimentation. Examples of suitable linear polyaromatic compoundsinclude 9,10-dimethylanthracene, 9,10-dichloroanthracene,9-methylanthracene, 9-acetylanthracene, 9-(methylaminomethyl)anthracene,2-choloranthracene, 2-ethyl-9,10-dimethoxyanthracene, anthrarobin, and9-anthryl trifluoromethyl ketone. The preferred linear polyaromaticcompounds are anthracene and 2,3-benzanthracene.

In a first reaction zone in step a), the feedstock composition,preferably an FT feedstock stream having an average carbon numberranging from C₆-C₁₈, is contacted with a linear polyaromatic compound.In the second reaction zone, the saturated hydrocarbon stream removedfrom the first reaction zone is also contacted with a linearpolyaromatic compound. In each reaction zone, the Diels-Alder adductforming reaction is carried out in a conventional fashion. Examples ofsuitable equipment in which the reactions are carried out include acontinuously stirred tank reactor, configured as a single unit, inparallel, or in series, wherein feedstock or an olefin composition, andlinear polyaromatic compound, are added continuously to a stirred tankto form a liquid reaction mixture under heat, and the reaction mixtureis continuously withdrawn from the stirred tank. Alternatively, thereaction may be carried out in a bubble column, or in a batch reactor,or utilizing a plug flow reaction scheme. The feedstock and olefincomposition adducting reactions are typically carried out over a rangeof temperatures from about 150° to about 290° C., preferably from about200° to about 280° C., and most preferably from about 240° to about 265°C. Pressures typically run from about atmospheric to about 100atmospheres. The reactions can be carried out in the gas phase undervacuum or liquid phase or mixed gas-liquid phase, depending on thevolatility of the feedstock, but generally in the liquid phase.

Stoichiometric ratios or an excess of either olefin or linearpolyaromatic compound can be used to form the adducts. The molar ratioof olefin to linear polyaromatic compound is preferably from 0.25:1 upto 10:1. Preferably, a molar excess of linear polyaromatic compounds isused to ensure a complete and large recovery of all olefins in the firstand second adduction zone.

The residence time is for a time sufficient to adduct the desired amountof linear polyaromatic compound with the olefin. Typical residence timesrange from 30 minutes to 4 hours in a batch reaction.

An inert solvent can be utilized to dissolve the feedstock olefins orthe linear polyaromatic compound or both in each of the adductingreactors. Preferred solvents are the hydrocarbon solvents which areliquid at reaction temperatures and in which the olefins, linearpolyaromatic compound and olefin-linear polyaromatic compound adductsare soluble. Illustrative examples of useful solvents include thealkanes such as pentane, iso-pentane, hexane, heptane, octane, nonane,and the like; cycloalkanes such as cyclopentane, cyclohexane, and thelike; and aromatics such as benzene, toluene, ethylbenzene,diethylbenzene, and the like. The amount of solvent to be employed canvary over a wide range without a deleterious effect on the reaction.

Preferably, the adducting reactions are carried out in the absence of asolvent, thereby improving the rate of reaction and avoid the need foradditional equipment and process steps for separating the solvent.

After formation of the linear polyaromatic compound-olefin adduct instep a), the adduct stream flows to a separation vessel effective forseparating the saturated hydrocarbons from the linear polyaromaticcompound-olefin adduct to form a saturated hydrocarbon stream and anolefin adducted stream in step b). Due to the large molecular weight andstructural difference between the adducts and the other ingredients inthe reaction mixtures, such as saturated hydrocarbons and internalolefins, conventional separation techniques are quite suitable forremoving the unreacted saturated hydrocarbons in step b) and internalolefins in step oiii) from the respective adducts. For example, thesaturated hydrocarbons in step b) and the internal olefins in step oiii)may be removed at the overhead or in fractions, by partial vacuum orflash distillation of the reaction mixture to leave the adducts andunreacted linear polyaromatic compounds as a liquid bottoms. It isdesirable to raise the temperature at the bottoms of the distillationcolumn sufficient to retain the bottoms in liquid state, while keepingthe temperature and residence time as low as possible to avoiddissociating the adducts. Suitable temperatures at the bottoms of theseparation vessel range from 210° C. to 280° C., more preferably from230° C. to 270° C. While the pressure is not particularly limited, andthe separation can be conducted under atmospheric pressure, it ispreferred to conduct the separation under slight vacuum, e.g. 200 mmHgto 700 mmHg, to reduce the operating temperature and the residence timewithin the separation vessel. The residence time within the vesselshould be short to avoid excessive dissociation of the adducts, such asfrom 1 to 30 minutes.

In step b), the unreacted saturated hydrocarbon stream distillateincludes paraffins and may include, if present in the feedstockcomposition, aromatics and oxygenates such as the alcohols, ketones,acids, along with internal and branched olefins which failed to adductwith the linear polyaromatic compound.

Alternatively, the adducts may be separated by cooling the reactionmixture until the adduct crystallizes out, followed by filtration orcentrifugation to remove the unreacted saturated hydrocarbons in stepb).

In most cases, any unreacted linear polyaromatic compound will separateout with the adduct in the adducted olefin stream and the adductedlinear alpha olefin stream. Other ingredients, such as small amounts ofhigher molecular weight unreacted olefins, internal olefins, andbranched olefins, may remain in the adducted olefin stream and theadducted linear alpha olefin stream.

The recovery of a stream in a separation operation is determined by themolar ratio of linear polyaromatic compound to olefins, the adductingresidence time, the temperature within the separation vessel, and mostimportantly, the residence time (rate of separation) of the reactionmixture in the separation vessel. To obtain a large olefin compositionrecovery, any one or a combination of the following variables areadjusted: a high linear polyaromatic compound to olefin molar ratio,e.g., >1, long residence times to ensure complete adduction, andmoderate distillation temperatures to avoid dissociating the adducts.

The rate of olefin recovery from the feedstock is not limited, andgenerally will depend upon the amount of olefin present in thefeedstock. In one embodiment, the rate of recovery of olefin adductsfrom the first separation vessel, in moles/unit time, range from 0.10 to0.40, more preferably from 0.15 to 0.35, each based upon a feedstockrate of 1.00. At these rates, from 40% to 100% of the olefins in thefeedstock may be recovered into the olefin composition. In anotherembodiment, the rate of recovery ranges from 0.20 to 0.30, based upon afeedstock rate of 1.00.

In general, the recovery of olefins from the feedstock ranges from 70%to 100%.

The linear polyaromatic compound-olefin adducts in the adducted streammay be dissociated in a dissociation zone. The dissociation process canbe accomplished by feeding the adducted olefin stream to a dissociationvessel where the adducted olefin stream is heated and pyrolyzed at atemperature of from about 200° to about 500° C., preferably from about300° to about 350° C., for a time sufficient to dissociate the adducts.The dissociation temperature can be further reduced below 200° C. bystripping olefin gas as it is liberated using an inert gas. Thepyrolysis frees the olefins from the linear polyaromatic compound. Oneor more dissociation vessels may be used in series to conduct thedissociation, and the dissociation vessels may also be operated under apartial vacuum up to superatmospheric pressures.

The linear polyaromatic compound may subsequently be separated from theresulting mixture by any conventional means, which may occursimultaneously with the pyrolysis operation, such as by vacuum or flashdistilling off the olefins along with any impurities at the pyrolysistemperatures, and removing the linear polyaromatic compound as a bottomsfrom the dissociation zone. The dissociation vessel may be operatedunder slight vacuum to lower the boiling point of the dissociated linearalpha olefin and at a temperature sufficient to dissociate the adduct.Other separation techniques include filtration and centrifugation.

The olefin composition, whether separated or in mixture with thedissociated linear polyaromatic compounds, is now enriched in theconcentration of olefins over the concentration of olefins feedstock.Likewise, when the saturated hydrocarbons are separated from the linearpolyaromatic compound-olefin adduct in the separation vessel as a firstsaturated hydrocarbon stream, the first saturated hydrocarbon stream isenriched in its concentration of saturated hydrocarbons over theconcentration of saturated hydrocarbons in the feedstock flowing to thefirst adduct reaction zone, and the concentration of olefins in thefirst saturated hydrocarbon stream is reduced over the concentration ofolefins in the feedstock entering the first adduct reaction zone.

In the next step of the process, step si), the first saturatedhydrocarbon stream comprising an enriched concentration of saturatedhydrocarbons and a reduced concentration of linear alpha olefins andinternal olefins, is contacted with linear polyaromatic compounds in asecond adducting reaction zone under conditions effective to form areaction mixture comprising second linear polyaromatic compound-olefinadducts and an second saturated hydrocarbon composition. Suitablereaction conditions and vessels include those used in the adductingreaction zone for the feedstock.

Once the second linear polyaromatic compound-linear alpha olefin adducthas been formed in the second reaction zone in step si), the adductstream flows to a separation vessel in step sii) effective forseparating the second linear polyaromatic compounds-olefin adducts fromthe saturated hydrocarbons to form an second saturated hydrocarbonstream enriched in the concentration of saturated hydrocarbons over theconcentration of saturated hydrocarbons in the first saturatedhydrocarbons stream, and a second linear polyaromatic compound-olefinadduct stream.

Suitable methods and conditions for separating the second adducts fromthe second reaction mixture include any of the methods used to removethe adducted olefins from the reaction mixture in the first separationzone. Preferably, the second reaction mixture is distilled and a secondsaturated hydrocarbon stream is removed at the overhead of thedistillation column, while the olefin adducts are removed from thecolumn as a liquid bottoms stream. The second saturated hydrocarbonstream includes some internal olefins and alpha olefins, but in reducedconcentrations over the concentration of these species in the firstsaturated hydrocarbon stream. However, the concentration of thesaturated hydrocarbons in the second saturated hydrocarbon stream isenriched over their concentration in the first saturated hydrocarbonstream.

The linear polyaromatic compound-olefin adducts in the olefin adductstream removed from step sii) are dissociated in step siii) in adissociation zone to form linear polyaromatic compounds and a secondolefin composition. Suitable methods and conditions for dissociating theadducts in the linear alpha olefins adduct stream include thedissociation conditions effective for dissociating the olefins adductsformed removed in the first separation zone.

For purposes of measuring the percentage reduction of a species in astream, the concentration (all concentrations determined on the basis ofthe total weight of all ingredients present in the stream in question)of the species or series of species in question contained in the productstream is subtracted from the concentration of the species or series ofspecies in question contained in the predecessor stream in question, thedifference then divided by the concentration of the same species in thepredecessor stream multiplied by 100. For purposes of measuring the %enrichment of a species in a stream, the concentration of the species orseries of species in the predecessor or feedstock stream is subtractedfrom the concentration of species or series of species in questioncontained in the product stream, the difference then divided by theconcentration of those same species present in the predecessor feedstockstream and multiplied by 100. For purposes of adding together a seriesof species, the sum total of the series in the predecessor stream isadded, and then the sum total of the species in the product stream areadded if the concentration of the particular species is enriched overthat particular species in the predecessor stream, and subtracted if theconcentration of the particular species is reduced from theconcentration in the predecessor stream. The total in the product streamis then compared to the total in the predecessor stream to determinewhether the total of the series in the product stream was enriched orreduced over the sum total in the predecessor stream. The appropriatecalculation mentioned above is then applied depending on whether theseries in the product stream were reduced or enriched.

The Concentration of Species in the Olefin Composition and FirstSaturated Hydrocarbon Stream Relative to the Concentration of Species inthe Feedstock

In one embodiment, the concentration of all olefins in the firstsaturated hydrocarbon stream are reduced through the process of theinvention by at least 15%, preferably at least 30%, more preferably atleast 40%, over the concentration of all the olefins in the feedstock.

Since the linear polyaromatic compound is more selective towardsadducting with linear alpha olefins relative to other olefins, theconcentration of linear alpha olefins in the first saturated hydrocarbonstream in another embodiment are reduced by at least 30%, morepreferably by at least 40%, most preferably by at least 50%, over theconcentration of linear alpha olefins present in the feedstock stream.

The concentration of saturated hydrocarbon in the first saturatedhydrocarbon stream is enriched over the concentration of saturatedhydrocarbon in the feedstock stream. In an embodiment of the invention,the concentration is enriched by at least 5%, preferably by at least10%, more preferably by at least 20%, and can be enriched by 100-400%,especially when the concentration of saturated hydrocarbon in thefeedstock is low. Generally, the degree of enrichment of saturatedhydrocarbon in the saturated hydrocarbon stream varies inversely withthe concentration of the saturated hydrocarbons in the particularfeedstock employed.

In another embodiment of the invention, the concentration of saturatedhydrocarbons in the olefin composition is reduced through the process ofthe invention in only one pass by at least 80%, preferably by at least90%, more preferably by at least 95% over the concentration of saturatedhydrocarbon in the feedstock, and most preferably by 100%.

The concentration of linear alpha olefins in the olefin composition isenriched over the concentration of linear alpha olefins present in thefeedstock stream. In an embodiment of the invention, the concentrationof linear alpha olefins present in the olefin composition is enriched byat least 30%, more preferably by at least 40%, most preferably by atleast 60%, over the concentration of linear alpha olefins present in thefeedstock composition. The process of the invention can achieveconcentrations of linear alpha olefin in the olefin composition higherthan 80 wt. %, more preferably at least 90 wt. %.

Further, the concentration of all olefins in the olefin composition isenriched over the concentration of all olefins in the feedstock stream.The degree of olefin enrichment varies inversely with the concentrationof olefins present in the feedstock. In a preferred aspect of thisembodiment, the concentration of all olefins in the olefin compositionis enriched by at least 40%, preferably by at least 60%.

The process of the invention is capable of separating olefins fromsaturated hydrocarbons in a feedstock consisting essentially ofsaturated hydrocarbons and olefins, resulting in a concentration ofolefins in the olefin composition ranging from 90% to 100%.

Enrichment and Reduction of Species in the Second Saturated HydrocarbonStream and the Second Olefin Composition Relative to the First SaturatedHydrocarbon Stream And the Feedstock

The process of the invention enriches the concentration of saturatedhydrocarbons in the second saturated hydrocarbon stream relative to boththe first saturated hydrocarbon stream and the feedstock. The degree ofenrichment is preferably at least 5%, more preferably at least 10%. Ingeneral, the degree of enrichment will not be extremely high at thisstage since the first adduction and separation highly concentrates theamount of saturated hydrocarbon in the first hydrocarbon stream.

The second olefin composition is enriched in linear alpha olefins overthe concentration of linear alpha olefins in the first saturatedhydrocarbon stream and in the feedstock, preferably by at least 50%,more preferably by at least 100%.

The concentration of internal olefins is also enriched in the secondolefin composition over the concentration of internal olefins in thefirst saturated hydrocarbon stream, preferably by at least 20%, morepreferably by at least 50%.

To further illustrate the invention, the FIGURE depicts a block flowdiagram in which each of blocks 1 and 2 represent the adduction,separation, and dissociation steps, and lines 1,2,3,4, and 5 representthe feed and product streams into and from each block. Block 1represents the first adduction zone, separation zone, and dissociationzone. Block 2 represents the second adduction zone, separation zone, anddissociation zone. Line 1 represents the composition of the feedstock,Line 2 represents the composition of the saturated hydrocarbon stream,Line 3 represents the olefin composition stream, Line 4 represents thesecond saturated hydrocarbon stream, and Line 5 represents thecomposition of the second olefin composition stream.

The modeled mass balances tabulated below illustrate one of theembodiments of the invention wherein the recovery of a highconcentration of linear alpha olefins in the olefin composition, andrecovery of internal olefins and alpha olefins from the first saturatedhydrocarbon stream is desirable. Table A tabulates the mass balancebased upon the quantity of each species in a feed and product stream,while Table B presents a mass balance based upon the concentration ofeach species in a feed and product stream. Table A results are reportedas moles/unit time, and Table B results are reported as a mole percentcomposition in each stream. The mass balances are on a calculated basisto illustrate the concept of the invention, and are based upon the useof anthracene as the linear polyaromatic compound and upon theassumptions noted below Table B.

TABLE A 1 2 3 4 5 Paraffins (linear/branched) 0.15 0.15 0.00 0.15 0.00Saturated alkyl aromatics 0.15 0.15 0.00 0.15 0.00 Saturated oxygenates0.15 0.15 0.00 0.15 0.00 Linear alpha olefins 0.20 0.06 0.14 0.00 0.06Linear 2-olefins 0.10 0.05 0.05 0.01 0.05 2-methyl 1-olefins 0.25 0.220.03 0.11 0.11 Total 1.00 0.79 0.21 0.57 0.21

TABLE B 1 2 3 4 5 Paraffins (linear/branched) 15% 19%  0% 26%  0%Saturated alkyl aromatics 15% 19%  0% 26%  0% Saturated oxygenates 15%19%  0% 26%  0% Linear alpha olefins 20%  8% 66%  1% 27% Linear2-olefins 10%  7% 22%  1% 22% 2-methyl 1-olefins 25% 28% 12% 20% 51%Assumptions: Block 1 recovery set at 70% of the Linear Alpha Olefins.Block 2 recovery set at 63% of all the olefins in Stream 2. Equilibriumis assumed at each stage. Assume the equipment is capable of perfectrejection of saturated hydrocarbons, aromatics, and oxygenates. Theratio of equilibrium constants between linear alpha olefins and linear2-olefins is set at 2.7. The ratio of equilibrium constants betweenlinear alpha olefins and 2-Methyl 1-Olefins is set at 20. In block 1,the percentage # of linear 2-olefin extracted from block 1 is 46%, andof the 2-methyl 1-olefin is 10%. In block 2, 88% of the linear 2-olefinsare extracted, and 49% of the 2-methyl 1-olefin are extracted, eachbased upon the amount of material entering block 2.

The mass balances tabulated below illustrate another modeled embodimentof the invention wherein the recovery of higher quantities, albeit atlower concentrations relative to the embodiment above, of linear alphaolefins in the linear alpha olefin stream is desirable. Table Ctabulates the mass balance based upon the quantity of each species in afeed and product stream, while Table D presents a mass balance basedupon the concentration of each species in a feed and product stream. Themass balances are on a calculated basis to illustrate the concept of theinvention, and are based upon the use of anthracene as the linearpolyaromatic compound and upon the assumptions noted below Table D.

TABLE C 1 2 3 4 5 Paraffins (linear/branched) 0.15 0.15 0.00 0.15 0.00Saturated alkyl aromatics 0.15 0.15 0.00 0.15 0.00 Saturated oxygenates0.15 0.15 0.00 0.15 0.00 Linear alpha olefins 0.20 0.03 0.17 0.00 0.03Linear 2-olefins 0.10 0.03 0.07 0.00 0.03 2-methyl 1-olefins 0.25 0.190.06 0.10 0.09 Total 1.00 0.71 0.29 0.56 0.15

TABLE D 1 2 3 4 5 Paraffins (linear/branched) 15% 21%  0% 27%  0%Saturated alkyl aromatics 15% 21%  0% 27%  0% Saturated oxygenates 15%21%  0% 27%  0% Linear alpha olefins 20%  4% 58%  0% 19% Linear2-olefins 10%  5% 23%  1% 19% 2-methyl 1-olefins 25% 28% 19% 18% 63%Assumptions: Block 1 recovery set at 85% of all the Linear AlphaOlefins. Block 2 recovery set at 59% of all the olefins in Stream 2.Equilibrium is assumed at each stage. Assume the equipment is capable ofperfect rejection of saturated hydrocarbons, aromatics, and oxygenates.The ratio of equilibrium constants between linear alpha olefins andlinear 2-olefins is set at 2.7. The ratio of equilibrium constantsbetween linear alpha olefins and 2-Methyl 1-Olefins is set at 20. Inblock 1, the # percentage of linear 2-olefin and 2-methyl 1-olefinextracted from block 1 is 68% and 22%, respectively. In block 2, thepercentage of the linear 2-olefins and 2-methyl 1-olefin extracted are88% and 49%, respectively, each based upon the amount of materialentering block 2.

Fisher-Tropsch streams contain a variety of difficult to separatespecies, including saturated hydrocarbons, aromatics, oxygenates,internal olefins, branched olefins, and linear alpha olefins. Anadvantage of a Fisher-Tropsch stream is that it contains a mixture ofboth even and odd carbon, and the process of the invention produces astream having even and odd carbon number olefin species with a very lowto zero amount of saturated hydrocarbons and high concentrations oflinear alpha olefins. The process of the invention can also provide aFisher-Tropsch olefin composition having a mixture of internal olefinsand/or branched olefins, and linear alpha olefins with low amounts ofsaturated hydrocarbons.

In one embodiment, the process of the invention provides a composition,preferably Fisher-Tropsch derived, comprising odd and even numberedolefins, an average carbon number ranging from C₅ to C₂₀, preferably C₆to C₁₈, or optionally in the C₆ to C₁₂ range, comprising:

a) at least two linear alpha olefin species having different carbonchain lengths;

b) the two most predominant (on a mole basis) linear alpha olefinspecies of the at least two linear alpha olefin species are each withinthe range of C₆ to C₁₈, or in the case of using a C₆ to C₁₂ feedstock,within that range, inclusive;

c) the two most predominant linear alpha olefin species are present inan amount of at least 20 wt %, preferably at least 30 wt. %, morepreferably at least 40 wt. %, based on the weight of the olefins in thecomposition;

d) cumulatively, the total amount of linear alpha olefins present in thecomposition within said range, inclusive, is at least 40 wt. %,preferably at least 60 wt. %, more preferably at least 70 wt. %, andeven 90 wt. % or more, based on the weight of the olefins in thecomposition;

e) one or more odd numbered olefins within the range present in anamount of at least 10 wt. %, preferably at least 20 wt. %, morepreferably at least 30 wt. %, and even 40 wt. % or more, cumulative;

f) a cumulative amount of aromatics, saturated hydrocarbons, andoxygenates of 10 wt. % or less, based on the weight of the composition;and preferably

g) 6 wt. % or less of branched olefins having branching at the C₂ or C₃position relative to the most proximate double bond, more preferably 4wt. % or less, based on the weight of the composition.

In another embodiment of the invention, the above mentioned compositionhas as one of the two most predominant olefin species an odd carbonnumber linear alpha olefin.

In another embodiment of the invention, there is provided a composition,preferably Fisher-Tropsch derived, having an average carbon numberranging from C₆ to C₁₈ comprising at least two linear alpha olefinspecies having different carbon chain lengths within said range,inclusive, at least 50 wt. % of linear alpha olefins, where thecomposition has a most predominant olefin species represented by ncarbon numbers, wherein the next most predominant olefin species haseither n+1 or n−1 carbon numbers; and wherein said composition comprises10 wt. % or less of saturated hydrocarbons; and preferably wherein saidcomposition has branched olefins containing branching at the C₂ or C₃positions, relative to the most proximate double bond, in an amount of 6wt. %, more preferably 4 wt. % or less, based on the weight of thecomposition.

The process of the invention advantageously provides an olefin streamwhich is highly concentrated in olefins, wherein the concentration ofolefins in the olefin composition may be at least 90% and up to 100%olefin purity in the olefin composition. The process of the inventionalso provides for the recovery of a second olefin composition from afirst saturated hydrocarbon stream, which second olefin composition isenriched in both linear alpha olefins and internal olefins.

The olefin composition stream and the second olefin composition areuseful as a component in drilling fluids, to react with elemental sulfurto make sulfurized products as extreme pressure agents in metal workingfluids, as a co-monomers for the polymerization of polyethylene, as anintermediate in making polyalpha olefins (PAO) used as a lubricant, as achlorination feed to make polychlorinated hydrocarbons in PVCapplications, to react with hydrogen sulfides to make primary andsecondary mercaptans as pharmaceutical intermediates and as additives tomodify the properties of rubber, as solvents, and as a precursor for themanufacture of plasticizer alcohols and detergent range alcohols andsurfactants, which may be derivatized into detergent range sulfates oralkoxysulfates for laundry liquids and powders, dishwashing powders andliquids, bar soap, shampoo, liquid hand soap, and hard surface cleaners.

The ranges and limitations provided in the instant specification andclaims are those which are believed to particularly point out anddistinctly claim the instant invention. It is, however, understood thatother ranges and limitations that perform substantially the samefunction in substantially the same manner to obtain the same orsubstantially the same result are intended to be within the scope of theinstant invention. The present invention will now be illustrated bymeans of the following illustrative embodiments and examples which areprovided for illustration and are not to be construed as limiting theinvention.

EXAMPLE 1

To illustrate the concept of the invention, a Fisher-Tropsch streamcomprised of the composition set forth in Table 1 was used as afeedstock. The FT composition was derived by passing syngas over a FTcatalyst and subsequently distilling products in the boiling point rangeof hexyl to undecyl hydrocarbons. This composition was used as the feed.Hydrocarbons in the C₇-C₁₀ were the most abundant.

0.14 moles of anthracene having a 95% purity and 62.5 g of the feedstockwere placed in an autoclave. The total olefin content of the chargedfeed was about 0.15 moles (19.8 g), for an olefin/anthracene molar ratioof 1.1:1. The autoclave was sealed and then purged with nitrogen. Theautoclave was heated to 255° C. for 5.6 hours to form the Diels-Alderadduct between the olefin and the anthracene. The autoclave contentswere stirred during heating.

Once the reaction was complete, the autoclave was cooled to 20° C. Theproduct mixture was transferred to a glass flask and the unreactedolefin, saturated hydrocarbons, and unreacted oxygenates were removed bydistillation as Product A. The composition of Product A was determinedby gas chromatographic analysis.

The material remaining in the flask consisted of some entrainedsaturated hydrocarbons, unreacted anthracene, and the anthracene-olefinadduct. The flask and its contents were then heated to a temperatureranging from 310-350° C. to dissociate the adduct to anthracene andProduct B described in Table 1 below. Product B was separated andisolated from the anthracene by distillation. 9.2 g of Product B wasrecovered. The composition of Product B was determined by gaschromatographic analysis.

The results indicate that Product A is enriched in saturatedhydrocarbons (alkanes) over the concentration of saturated hydrocarbonsin the feedstock stream, by 24%. The concentration of alpha olefin inthe Product A stream was reduced by 55% over the concentration of alphaolefin in the feedstock.

Product B is greatly enriched in alpha olefin content and overall olefincontent over the concentration of alpha olefin and overall olefincontent in the feedstock stream. Product B is enriched in alpha olefincontent by 202%, and in overall olefin content, Product A was enrichedby 197% ([(88.21+5.77)−(27.18+4.43)]/(27.18+4.43)×100).

Further, the concentration of saturated hydrocarbon (alkane)in Product Bstream was greatly reduced; by 95%. The presence of saturatedhydrocarbons in Product B is due to its incomplete removal upondistillation of the unreacted material from the adduct before thedissociation step.

TABLE 1 SEPARATION OF SATURATED HYDROCARBONS FROM OLEFINS TOTAL INTERNALALPHA WEIGHT ALKANES OLEFINS OLEFINS OXYGENATES UNKOWNS COMPOSITION (g)(wt. %) (wt. %) (w %) (wt. %) (wt. %) Feedstock 62.5 63.8  4.43 27.183.06 1.45 Product A 44.3 79.25 4.6  12.23 3.01 0.91 Product B  9.3  3.315.77 88.21 2.0  0.81

The concentration of saturated hydrocarbons in Product A stream wasenhanced, and the concentration of internal olefins in the Product Astream was enhanced, by separating a portion of the internal olefin inProduct A stream from the saturated hydrocarbons.

44.3 g of Product A containing 7.5 g (0.059 moles) of olefin was treatedwith 0.034 moles of anthracene for 6 hours at 255° C. in the equipmentnoted above. The molar ratio of olefin to anthracene was 1.7:1. 30.24 gof unreacted material was removed by distillation as Product C stream.The bottoms of the distillation column was thermally dissociated at310-350° C. as described above. 1.67 g of the resulting Product Dinternal olefin stream was removed by distillation from the dissociatedanthracene. Each of Product C and D were analyzed by gas chromatography.The results are reported in Table 2.

Product C, compared to the feedstock stream Product A, was enriched inalkanes by 6.8%. The concentration of internal olefin in Product C,compared to the feedstock Product A stream, was decreased by 25%.

Product D was enriched in internal olefins and in alpha olefins over theconcentration of each olefin in the feedstock Product A stream. Theinternal olefin enrichment was about 98%, and the alpha olefinenrichment was about 570%.

TABLE 2 SEPARATION OF INTERNAL OLEFINS FROM SATURATED HYDROCARBONS TOTALINTERNAL ALPHA WEIGHT ALKANES OLEFINS OLEFINS OXYGENATES UNKOWNSCOMPOSITION (g) (wt. %) (wt. %) (w %) (wt. %) (wt. %) Product A 44.3 79.25 4.6  12.23 3.01 0.91 Feedstock Product C 30.24 85.04 6.03 6.541.63 0.76 Product D  1.67  6.80 9.11 82 1.26 0.83

What we claim is:
 1. A process for contacting a linear polyaromatic compound with a feedstock composition comprising linear alpha olefins, internal olefins, and saturated hydrocarbons, separating the olefins from the saturated hydrocarbons in the feedstock composition to form an olefin composition and a saturated hydrocarbon stream, subsequently contacting a linear polyaromatic compound saturated hydrocarbon stream comprising linear alpha olefins and internal olefins, and separating the internal olefins and linear alpha olefins from the saturated hydrocarbons in the saturated hydrocarbon stream to form a second saturated hydrocarbon stream and a second olefin composition, whereby the concentration of each of internal olefins and linear alpha olefins in the second olefin composition is enriched over the concentration of each of internal olefins and linear alpha olefins in the feedstock and in the olefin composition.
 2. The process of claim 1, wherein the average carbon number of the feedstock ranges from C₅-C₂₀ and wherein the predominant olefin species in the feedstock is within said range, inclusive.
 3. The process of claim 2, wherein the average carbon number of the feedstock ranges from C₆-C₁₈ and wherein the predominant olefin species in the feedstock is within said range, inclusive.
 4. The process of claim 3, wherein the linear polyaromatic compound comprises substituted or unsubstituted anthracene or benzanthranene.
 5. A process for contacting a linear polyaromatic compound with a feedstock composition comprising a fischer tropsch stream, separating the olefins from saturated hydrocarbons in the feedstock composition to form an olefin composition and a saturated hydrocarbon stream, subsequently contacting a linear polyaromatic compound with the saturated hydrocarbon stream comprising linear alpha olefins and internal olefins, and separating the internal olefins and linear alpha olefins from the saturated hydrocarbons in the saturated hydrocarbon stream to form a second saturated hydrocarbon stream and a second olefin composition, whereby the concentration of each of internal olefins and linear alpha olefins in the second olefin composition is enriched over the concentration of each of internal olefins and linear alpha olefins in the feedstock and in the olefin composition.
 6. The process of claim 5, wherein the feedstock comprises a single carbon cut composition.
 7. The process of claim 1 wherein said feedstock composition is contacted with said linear polyaromatic compound at a temperature of from 150° to about 290° C.
 8. The process of claim 1 wherein said feedstock composition is contacted with said linear polyaromatic compound at a temperature of from about 240° to about 265° C.
 9. The process of claim 1 wherein said olefins in said feedstock composition are at a molar ratio to said linear polyaromatic compounds of from about 0.25:1 to about 10:1.
 10. The process of claim 7 wherein said olefins in said feedstock composition are at a molar ratio to said linear polyaromatic compounds of from about 0.25:1 to about 10:1.
 11. The process of claim 8 wherein said olefins in said feedstock composition are at a molar ratio to said linear polyaromatic compounds of from about 0.25:1 to about 10:1.
 12. The process of claim 1 wherein linear polyaromatic compound-olefin adduct formed in said feedstock composition is dissociated by heating said linear polyaromatic compound-olefin adduct to a temperature ranging from about 200° C. to 500° C.
 13. The process of claim 7 wherein linear polyaromatic compound-olefin adduct formed in said feedstock composition is dissociated by heating said linear polyaromatic compound-olefin adduct to a temperature ranging from about 200° C. to 500° C.
 14. The process of claim 8 wherein linear polyaromatic compound-olefin adduct formed in said feedstock composition is dissociated by heating said linear polyaromatic compound-olefin adduct to a temperature ranging from about 200° C. to 500° C.
 15. The process of claim 9 wherein linear polyaromatic compound-olefin adduct formed in said feedstock composition is dissociated by heating said linear polyaromatic compound-olefin adduct to a temperature ranging from about 200° C. to 500° C.
 16. The process of claim 10 wherein linear polyaromatic compound-olefin adduct formed in said feedstock composition is dissociated by heating said linear polyaromatic compound-olefin adduct to a temperature ranging from about 200° C. to 500° C.
 17. The process of claim 12 wherein linear polyaromatic compound-olefin adduct formed in said feedstock composition is dissociated by heating said linear polyaromatic compound-olefin adduct to a temperature ranging from about 200° C. to 500° C.
 18. The process of claim 12 wherein said linear polyaromatic compound-olefin adduct is heated to a temperature ranging from about 300° C. to 350° C.
 19. The process of claim 16 wherein said linear polyaromatic compound-olefin adduct is heated to a temperature ranging from about 300° C. to 350° C.
 20. The process of claim 17 wherein said linear polyaromatic compound-olefin adduct is heated to a temperature ranging from about 300° C. to 350° C.
 21. The process of claim 1 wherein said linear polyaromatic compound is separated from the olefin composition by vacuum or flash distillation.
 22. The process of claim 12 wherein the linear polyaromatic compound is separated from the olefin composition by vacuum or flash distillation.
 23. The process of claim 19 wherein the linear polyaromatic compound is separated from the olefin composition by vacuum or flash distillation.
 24. The process of claim 20 wherein the linear polyaromatic compound is separated from the olefin composition by vacuum or flash distillation.
 25. The process of claim 1 wherein the feedstock composition comprises from 15 wt. % to 70 wt. % olefin, based on the weight of all ingredients in the feedstock.
 26. The process of claim 1 wherein the feedstock composition comprises from 15 wt. % to 65 wt. % linear alpha olefin, based on the weight of all ingredients in the feedstock.
 27. The process of claim 1 wherein the feedstock composition comprises from 5 wt. % to 65 wt. %. paraffin, based on the weight of all ingredients in said feedstock composition.
 28. The process of claim 1 wherein the amount of all olefins in the feedstock composition other than linear alpha olefins ranges from 5 wt. % to 45 wt. %, based on the weight of all ingredients in said feedstock composition.
 29. The process of claim 1 wherein the amount of paraffin ranges from 65 to 99 wt. % of all ingredients in said feedstock composition.
 30. The process of claim 1 wherein the average carbon number of said feedstock composition ranges from C₅-C₂₀ and wherein the predominant olefin species in said feedstock composition is within said range, inclusive.
 31. The process of claim 1 wherein the average carbon number of said feedstock composition ranges from C₆-C₁₈ and wherein the predominant olefin species in said feedstock composition is within said range, inclusive.
 32. The process of claim 1 wherein said linear polyaromatic compound has a greater selectivity for linear alpha olefin compounds over other olefins in an amount of greater than 2:1 by mole.
 33. The process of claim 7 wherein said linear polyaromatic compound has a greater selectivity for linear alpha olefin compounds over other olefins in an amount of greater than 2:1 by mole.
 34. The process of claim 8 wherein said linear polyaromatic compound has a greater selectivity for linear alpha olefin compounds over other olefins in an amount of greater than 2:1 by mole.
 35. The process of claim 9 wherein said linear polyaromatic compound has a greater selectivity for linear alpha olefin compounds over other olefins in an amount of greater than 2:1 by mole.
 36. The process of claim 10 wherein said linear polyaromatic compound has a greater selectivity for linear alpha olefin compounds over other olefins in an amount of greater than 2:1 by mole.
 37. The process of claim 16 wherein said linear polyaromatic compound has a greater selectivity for linear alpha olefin compounds over other olefins in an amount of greater than 2:1 by mole.
 38. The process of claim 1 wherein said linear polyaromatic compound is selected from the group consisting of substituted and unsubstituted anthracene and benzanthracene, wherein said substituted anthracene and benzanthracene comprise substitutents which are sufficiently inert and insufficiently large to interfere with formation of a Diels Alder adduct between said linear polyaromatic compound and olefins in said feedstock composition.
 39. The process of claim 7 wherein said linear polyaromatic compound is selected from the group consisting of substituted and unsubstituted anthracene and benzanthracene, wherein said substituted anthracene and benzanthracene comprise substitutents which are sufficiently inert and insufficiently large to interfere with formation of a Diels Alder adduct between said linear polyaromatic compound and olefins in said feedstock composition.
 40. The process of claim 8 wherein said linear polyaromatic compound is selected from the group consisting of substituted and unsubstituted anthracene and benzanthracene, wherein said substituted anthracene and benzanthracene comprises substitutents which are sufficiently inert and insufficiently large to interfere with formation of a Diels Alder adduct between said linear polyaromatic compound and olefins in said feedstock composition.
 41. The process of claim 9 wherein said linear polyaromatic compound is selected from the group consisting of substituted and unsubstituted anthracene and benzanthracene, wherein said substituted anthracene and benzanthracene comprise substitutents which are sufficiently inert and insufficiently large to interfere with formation of a Diels Alder adduct between said linear polyaromatic compound and olefins in said feedstock composition.
 42. The process of claim 10 wherein said linear polyaromatic compound is selected from the group consisting of substituted and unsubstituted anthracene and benzanthracene, wherein said substituted anthracene and benzanthracene comprise substitutents which are sufficiently inert and insufficiently large to interfere with formation of a Diels Alder adduct between said linear polyaromatic compound and olefins in said feedstock composition.
 43. The process of claim 16 wherein said linear polyaromatic compound is selected from the group consisting of substituted and unsubstituted anthracene and benzanthracene, wherein said substituted anthracene and benzanthracene comprise substitutents which are sufficiently inert and insufficiently large to interfere with formation of a Diels Alder adduct between said linear polyaromatic compound and olefins in said feedstock composition.
 44. The process of claim 1 wherein said linear polyaromatic compound comprises unsubstituted anthracene.
 45. The process of claim 7 wherein said linear polyaromatic compound comprises unsubstituted anthracene.
 46. The process of claim 8 wherein said linear polyaromatic compound comprises unsubstituted anthracene.
 47. The process of claim 9 wherein said linear polyaromatic compound comprises unsubstituted anthracene.
 48. The process of claim 10 wherein said linear polyaromatic compound comprises unsubstituted anthracene.
 49. The process of claim 16 wherein said linear polyaromatic compound comprises unsubstituted anthracene.
 50. The process of claim 1 wherein the rate of olefin recovery from said feedstock composition ranges from 0.10 to 0.4 moles/unit time based on a feed rate of 1.0 moles/unit time.
 51. The process of claim 7 wherein the rate of olefin recovery from said feedstock composition ranges from 0.10 to 0.4 moles/unit time based on a feed rate of 1.0 moles/unit time.
 52. The process of claim 8 wherein the rate of olefin recovery from said feedstock composition ranges from 0.10 to 0.4 moles/unit time based on a feed rate of 1.0 moles/unit time.
 53. The process of claim 9 wherein the rate of olefin recovery from said feedstock composition ranges from 0.10 to 0.4 moles/unit time based on a feed rate of 1.0 moles/unit time.
 54. The process of claim 10 wherein the rate of olefin recovery from said feedstock composition ranges from 0:10 to 0.4 moles/unit time based on a feed rate of 1.0 moles/unit time.
 55. The process of claim 16 wherein the rate of olefin recovery from said feedstock composition ranges from 0.10 to 0.4 moles/unit time based on a feed rate of 1.0 moles/unit time.
 56. The process of claim 1 wherein the recovery of olefins from the feedstock ranges from 40 to 100%.
 57. The process of claim 7 wherein the recovery of olefins from the feedstock ranges from 40 to 100%.
 58. The process of claim 8 wherein the recovery of olefins from the feedstock ranges from 40 to 100%.
 59. The process of claim 9 wherein the recovery of olefins from the feedstock ranges from 40 to 100%.
 60. The process of claim 10 wherein the recovery of olefins from the feedstock ranges from 40 to 100%.
 61. The process of claim 16 wherein the recovery of olefins from the feedstock ranges from 40 to 100%.
 62. The process of claim 1 wherein the second saturated hydrocarbon stream is enriched in saturated hydrocarbons by at least 10%.
 63. The process of claim 1 wherein the concentration of linear alpha olefins in the saturated hydrocarbon stream is reduced in one pass by at least 40% over the concentration of linear alpha olefins present in said feedstock composition.
 64. The process of claim 1 wherein said feedstock composition comprises a single carbon cut composition.
 65. The process of claim 1 wherein said feedstock composition comprises a single cut C₆, C₈, C₉, C₁₀, C₁₁, C₁₂, C₁₄, or C₁₆ composition.
 66. The process of claim 1 wherein the concentration of saturated hydrocarbons in said second saturated hydrocarbon stream is enriched by at least 5% relative to the concentration of saturated hydrocarbons in said feedstock composition.
 67. The process of claim 1 wherein the concentration of internal olefins in said second saturated hydrocarbon stream is reduced by at least 20% relative to the concentration of saturated hydrocarbons in said feedstock composition.
 68. The process of claim 1 wherein the concentration of internal olefins in said second olefin composition is enriched by at least 50% relative to the concentration of saturated hydrocarbons in said feedstock composition.
 69. The process of claim 1 wherein the concentration of linear alpha olefins present in said second olefin composition is enriched by at least 100% relative to the concentration of saturated hydrocarbons in said feedstock composition.
 70. The process of claim 5 wherein said feedstock composition is contacted with said linear polyaromatic compound at a temperature of from 150° to about 290° C.
 71. The process of claim 5 wherein said feedstock composition is contacted with said linear polyaromatic compound at a temperature of from about 240° to about 265° C.
 72. The process of claim 5 wherein said olefins in said feedstock composition are at a molar ratio to said linear polyaromatic compounds of from about 0.25:1 to about 10:1.
 73. The process of claim 70 wherein said olefins in said feedstock composition are at a molar ratio to said linear polyaromatic compounds of from about 0.25:1 to about 10:1.
 74. The process of claim 71 wherein said olefins in said feedstock composition are at a molar ratio to said linear polyaromatic compounds of from about 0.25:1 to about 10:1.
 75. The process of claim 5 wherein linear polyaromatic compound-olefin adduct formed in said feedstock composition is dissociated by heating said linear polyaromatic compound-olefin adduct to a temperature ranging from about 200° C. to 500° C.
 76. The process of claim 70 wherein linear polyaromatic compound-olefin adduct formed in said feedstock composition is dissociated by heating said linear polyaromatic compound-olefin adduct to a temperature ranging from about 200° C. to 500° C.
 77. The process of claim 71 wherein linear polyaromatic compound-olefin adduct formed in said feedstock composition is dissociated by heating said linear polyaromatic compound-olefin adduct to a temperature ranging from about 200° C. to 500° C.
 78. The process of claim 72 wherein linear polyaromatic compound-olefin adduct formed in said feedstock composition is dissociated by heating said linear polyaromatic compound-olefin adduct to a temperature ranging from about 200° C. to 500° C.
 79. The process of claim 73 wherein linear polyaromatic compound-olefin adduct formed in said feedstock composition is dissociated by heating said linear polyaromatic compound-olefin adduct to a temperature ranging from about 200° C. to 500° C.
 80. The process of claim 74 wherein linear polyaromatic compound-olefin adduct formed in said feedstock composition is dissociated by heating said linear polyaromatic compound-olefin adduct to a temperature ranging from about 200° C. to 500° C.
 81. The process of claim 75 wherein said linear polyaromatic compound-olefin adduct is heated to a temperature ranging from about 300° C. to 350° C.
 82. The process of claim 76 wherein said linear polyaromatic compound-olefin adduct is heated to a temperature ranging from about 300° C. to 350° C.
 83. The process of claim 77 wherein said linear polyaromatic compound-olefin adduct is heated to a temperature ranging from about 300° C. to 350° C.
 84. The process of claim 5 wherein said linear polyaromatic compound is separated from the olefin composition by vacuum or flash distillation.
 85. The process of claim 79 wherein the linear polyaromatic compound is separated from the olefin composition by vacuum or flash distillation.
 86. The process of claim 80 wherein the linear polyaromatic compound is separated from the olefin composition by vacuum or flash distillation.
 87. The process of claim 83 wherein the linear polyaromatic compound is separated from the olefin composition by vacuum or distillation.
 88. The process of claim 5 wherein said linear polyaromatic compound has a greater selectivity for linear alpha olefin compounds over other olefins in an amount of greater than 2:1 by mole.
 89. The process of claim 70 wherein said linear polyaromatic compound has a greater selectivity for linear alpha olefin compounds over other olefins in an amount of greater than 2:1 by mole.
 90. The process of claim 71 wherein said linear polyaromatic compound has a greater selectivity for linear alpha olefin compounds over other olefins an amount of greater than 2:1 by mole.
 91. The process of claim 72 wherein said linear polyaromatic compound has a greater selectivity for linear alpha olefin compounds over other olefins in an amount of greater than 2:1 by mole.
 92. The process of claim 73 wherein said linear polyaromatic compound has a greater selectivity for linear alpha olefin compounds over other olefins in an amount of greater than 2:1 by mole.
 93. The process of claim 74 wherein said linear polyaromatic compound has a greater selectivity for linear alpha olefin compounds over other olefins in an amount of greater than 2:1 by mole.
 94. The process of claim 70 wherein said linear polyaromatic compound is selected from the group consisting of substituted and unsubstituted anthracene and benzanthracene, wherein said substituted anthracene and benzanthracene comprise substitutents which are sufficiently inert and insufficiently large to interfere with formation of a Diels Alder adduct between said linear polyaromatic compound and olefins in said feedstock composition.
 95. The process of claim 71 wherein said linear polyaromatic compound is selected from the group consisting of substituted and unsubstituted anthracene and benzanthracene, wherein said substituted anthracene and benzanthracene comprise substitutents which are sufficiently inert and insufficiently large to interfere with formation of a Diels Alder adduct between said linear polyaromatic compound and olefins in said feedstock composition.
 96. The process of claim 72 wherein said linear polyaromatic compound is selected from the group consisting of substituted and unsubstituted anthracene and benzanthracene, wherein said substituted anthracene and benzanthracene comprise substitutents which are sufficiently inert and insufficiently large to interfere with formation of a Diels Alder adduct between said linear polyaromatic compound and olefins in said feedstock composition.
 97. The process of claim 73 wherein said linear polyaromatic compound is selected from the group consisting of substituted and unsubstituted anthracene and benzanthracene, wherein said substituted anthracene and benzanthracene comprise substitutents which are sufficiently inert and insufficiently large to interfere with formation of a Diels Alder adduct between said linear polyaromatic compound and olefins in said feedstock composition.
 98. The process of claim 74 wherein said linear polyaromatic compound is selected from the group consisting of substituted and unsubstituted anthracene and benzanthracene, wherein said substituted anthracene and benzanthracene comprise substitutents which are sufficiently inert and insufficiently large to interfere with formation of a Diels Alder adduct between said linear polyaromatic compound and olefins in said feedstock composition.
 99. The process of claim 5 wherein said linear polyaromatic compound comprises unsubstituted anthracene.
 100. The process of claim 70 wherein said linear polyaromatic compound comprises unsubstituted anthracene.
 101. The process of claim 71 wherein said linear polyaromatic compound comprises unsubstituted anthracene.
 102. The process of claim 72 wherein said linear polyaromatic compound comprises unsubstituted anthracene.
 103. The process of claim 73 wherein said linear polyaromatic compound comprises unsubstituted anthracene.
 104. The process of claim 74 wherein said linear polyaromatic compound comprises unsubstituted anthracene.
 105. The process of claim 5 wherein the rate of olefin recovery from said feedstock composition ranges from 0.10 to 0.4 moles/unit time based on a feed rate of 1.0 moles/unit time.
 106. The process of claim 70 wherein the rate of olefin recovery from said feedstock composition ranges from 0.10 to 0.4 moles/unit time based on a feed rate of 1.0 moles/unit time.
 107. The process of claim 71 wherein the rate of olefin recovery from said feedstock composition ranges from 0.10 to 0.4 molels/unit time based on a feed rate of 1.0 moles/unit time.
 108. The process of claim 72 wherein the rate of olefin recovery from said feedstock composition ranges from 0.10 to 0.4 moles/unit time based on a feed rate of 1.0 moles/unit time.
 109. The process of claim 73 wherein the rate of olefin recovery from said feedstock composition ranges from 0.10 to 0.4 moles/unit time based on a feed rate of 1.0 moles/unit time.
 110. The process of claim 74 wherein the rate of olefin recovery from said feedstock composition ranges from 0.10 to 0.4 moles/unit time based on a feed rate of 1.0 moles/unit time.
 111. The process of claim 5 wherein the recovery of olefins from the feedstock ranges from 40 to 100%.
 112. The process of claim 70 wherein the recovery of olefins from the feedstock ranges from 40 to 100%.
 113. The process of claim 71 wherein the recovery of olefins from the feedstock ranges from 40 to 100%.
 114. The process of claim 72 wherein the recovery of olefins from the feedstock ranges from 40 to 100%.
 115. The process of claim 73 wherein the recovery of olefins from the feedstock ranges from 40 to 100%.
 116. The process of claim 74 wherein the recovery of olefins from the feedstock ranges from 40 to 100%.
 117. The process of claim 5 wherein the second saturated hydrocarbon stream is enriched in saturated hydrocarbons by at least 10%.
 118. The process of claim 5 wherein the concentration of linear alpha olefins in the saturated hydrocarbon stream is reduced in one pass by at least 40% over the concentration of linear alpha olefins present in said feedstock composition.
 119. The process of claim 5 wherein the concentration of saturated hydrocarbons in said second saturated hydrocarbon stream is enriched by at least 5% relative to the concentration of saturated hydrocarbons in said feedstock composition.
 120. The process of claim 5 wherein the concentration of internal olefins in said second saturated hydrocarbon stream is reduced by at least 20% relative to the concentration of saturated hydrocarbons in said feedstock composition.
 121. The process of claim 5 wherein the concentration of internal olefins in said second olefin composition is enriched by at least 50% relative to the concentration of saturated hydrocarbons in said feedstock composition.
 122. The process of claim 5 wherein the concentration of linear alpha olefins present in said second olefin composition is enriched by at least 100% relative to the concentration of saturated hydrocarbons in said feed stock composition.
 123. A process for treating a feedstock composition comprising: contacting a linear polyaromatic compound with a feedstock composition comprising a Fischer Tropsch stream; separating olefins from saturated hydrocarbons in said feedstock composition to form an olefin composition and a saturated hydrocarbon stream, subsequently contacting the saturated hydrocarbon stream comprising linear alpha olefins and internal olefins with a linear polyaromatic compound selected from the group consisting of substituted and unsubstituted anthracene and benzanthracene, wherein said substituted anthracene and benzanthracene comprise substitutents which are sufficiently inert and insufficiently large to interfere with formation of a Diels Alder adduct between said linear polyaromatic compound and olefins in said feedstock composition; and separating the internal olefins and linear alpha olefins from the saturated hydrocarbons in the saturated hydrocarbon stream to form a second saturated hydrocarbon stream and a second olefin composition; whereby the concentration of each of internal olefins and linear alpha olefins in the second olefin composition is enriched over the concentration of each of internal olefins and linear alpha olefins in the feedstock and in the olefin composition.
 124. The process of claim 123 wherein said linear polyaromatic compound comprises unsubstituted anthracene.
 125. The process of claim 123 wherein said feedstock composition is contacted with said linear polyaromatic compound at a temperature of from 150° to about 290° C.
 126. The process of claim 124 wherein said feedstock composition is contacted with said linear polyaromatic compound at a temperature of from 150° to about 290° C.
 127. The process of claim 123 wherein said feedstock composition is contacted with said linear polyaromatic compound at a temperature of from about 240° to about 265° C.
 128. The process of claim 123 wherein said olefins in said feedstock composition are at a molar ratio to said linear polyaromatic compounds of from about 0.25:1 to about 10:1.
 129. The process of claim 124 wherein said olefins in said feedstock composition are at a molar ratio to said linear polyaromatic compounds of from about 0.25 to about 10:1.
 130. The process of claim 126 wherein said olefins in said feedstock composition are at a molar ratio to said linear polyaromatic compounds of from about 0.25:1 to about 10:1.
 131. The process of claim 123 wherein linear polyaromatic compound-olefin adduct formed in said feedstock composition is dissociated by heating said linear polyaromatic compound-olefin adduct to a temperature ranging from about 200° C. to 500° C.
 132. The process of claim 124 wherein linear polyaromatic compound-olefin adduct formed in said feedstock composition is dissociated by heating said linear polyaromatic compound-olefin adduct to a temperature ranging from about 200° C. to 500° C.
 133. The process of claim 125 wherein linear polyaromatic compound-olefin adduct formed in said feedstock composition is dissociated by heating said linear polyaromatic compound-olefin adduct to a temperature ranging from about 200° C. to 500° C.
 134. The process of claim 126 wherein linear polyaromatic compound-olefin adduct formed in said feedstock composition is dissociated by heating said linear polyaromatic compound-olefin adduct to a temperature ranging from about 200° C. to 500° C.
 135. The process of claim 123 wherein said linear polyaromatic compound-olefin adduct is heated to a temperature ranging from about 300° C. to 350° C.
 136. The process of claim 123 wherein said linear polyaromatic compound is separated from the olefin composition by vacuum or flash distillation.
 137. The process of claim 124 wherein the linear polyaromatic compound is separated from the olefin composition by vacuum or flash distillation.
 138. The process of claim 125 wherein the linear polyaromatic compound is separated from the olefin composition by vacuum or flash distillation.
 139. The process of claim 126 wherein the linear polyaromatic compound is separated from the olefin composition by vacuum or flash distillation.
 140. The process of claim 123 wherein said linear polyaromatic compound has a greater selectivity for linear alpha olefin compounds over other olefins in an amount of greater than 2:1 by mole.
 141. The process of claim 125 wherein said linear polyaromatic compound has a greater selectivity for linear alpha olefin compounds over other olefins in an amount of greater than 2:1 by mole.
 142. The process of claim 127 wherein said linear polyaromatic compound has a greater selectivity for linear alpha olefin compounds over other olefins in an amount of greater than 2:1 by mole.
 143. The process of claim 123 wherein the rate of olefin recovery from said feedstock composition ranges from 0.10 to 0.4 moles/unit time based on a feed rate of 1.0 moles/unit time.
 144. The process of claim 123 wherein the recovery of olefins from the feedstock ranges from 40 to 100%.
 145. The process of claim 123 wherein the second saturated hydrocarbon stream is enriched in saturated hydrocarbons by at least 10%.
 146. The process of claim 123 wherein the concentration of linear alpha olefins in the saturated hydrocarbon stream-is reduced in one pass by at least 40% over the concentration of linear alpha olefins present in said feedstock composition.
 147. The process of claim 123 wherein the concentration of saturated hydrocarbons in said second saturated hydrocarbon stream is enriched by at least 5% relative to the concentration of saturated hydrocarbons in said feedstock composition.
 148. The process of claim 123 wherein the concentration of internal olefins in said second saturated hydrocarbon stream is reduced by at least 20% relative to the concentration of saturated hydrocarbons in said feedstock composition.
 149. The process of claim 123 wherein the concentration of internal olefins in said second olefin composition is enriched by at least 50% relative to the concentration of saturated hydrocarbons in said feedstock composition.
 150. The process of claim 123 wherein the concentration of linear alpha olefins present in said second olefin composition is enriched by at least 100% relative to the concentration of saturated hydrocarbons in said feedstock composition. 